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'.... I~ co ~ C\l c. ,-- .....' ~~ ", . One 8,000,000 gal Ion membrane I ined neutral ization basin with three 800 gpm pumps . Two 550 gpm vapor compression evaporators and one 300 gpm brine vapor compression evaporators with deaerators, chemical storage and feed systems, control room and product storage ':: ", . 34 acres of membrane I ined evaporation ponds with 15 foot depth .. EquIpment Cost Sllmmary :'- The total capital cost for water system equipment ment, engineering and installation/construction. summarized on Table 5-1. and ponds includes equip- These estimated costs are <; CHEMICAL COSTS The estimated cost of chemicals FOB the on Table 5-2. The chemical consumption capacity factor of 76% is summarized on rates are shown in the process flow and Harry Allen plant site are summarized cost for each option at a plant Table 5-3. The annual chemical usage material balances found in Appendix C. POWER USAGE Annual power usage is based on a 76% capacity factor, assuming 5 kwh/l,OOO gallons for cool ing water system pumping and 90 kwh/l,OOO gallons for water treated by the brine concentrators. Power usage for the five options is shown on Table 5-4. The energy cost factor provided by Nevada Power Company in- cludes both energy and demand and is addressed in the comparison of total levelized costs. OPERATING LABOR AND MAINTENANCE COSTS Operating and maintenance costs are based on a labor rate of $50,000 per manyear, 0.75% of total capital cost for repair materials and 0.3% of total capital cost for maintenance labor. An additional labor cost of $100,000 per manyear was added to the ion exchange softening configuration (Option I) to account for a higher degree of technical support than the other options. The estimated annual operating and maintenance costs are presented In Table 5-5. (~ ".": .~. 5-4 :'~ ,. ;~ :::i r.' , "